ES2362368T3 - EXTRACTION OF BIOPOLYMERS FROM VEGETABLE MATERIALS. - Google Patents

Abstract

Disclosed is a method and apparatus for the extraction of high molecular weight biopolymers from plants. Specifically, invention described herein relates to the commercial processing of plant material, including that from desert plants native to the southwestern United States and Mexico, such as the guayule plant (Parthenium argentatum), for the extraction of biopolymers, including natural rubbers. More specifically, the invention relates to laboratory to commercial scale extraction of high molecular weight biopolymers from plant materials including the chemical and mechanical processing of the plants and purification of the extracted biopolymer.

Description

FIELD OF THE INVENTION

The invention described herein refers to the commercial processing of native desert plants of the southwest of the United States of America and Mexico, including the guayule (Parthenium argentatum), for the extraction of biopolymers such as natural rubbers. More specifically, the invention relates to the production method, on a commercial scale, of extracting a high molecular weight biopolymer from plant materials, including cultivation, harvesting, desfoliation and descortization, and chemical and mechanical treatment of the plants.

BACKGROUND OF THE INVENTION

Natural rubber, derived from the Hevea brasiliensis plant, is a fundamental component of many consumer goods, including medical devices and products, such as latex gloves. The United States of America has a strong dependence on natural rubber, mainly because synthetic alternatives cannot match the high behavioral properties of natural rubber required for many applications, and tend to be prohibitively expensive.

More than 90% of the natural rubber derived from Hevea imported by the United States of America comes from Indonesia, Malaysia and Thailand. The sources of natural rubbers in these countries are under an intense threat of diseases and potential pests, due to the genetic similarity of rubber plants. In addition, the harvest is limited by a restricted geographical area and by collection methods that require a lot of labor. In addition, natural rubber crops in Southeast Asia contain many protein contaminants that are responsible for allergies to latex type I, estimated to affect as many as 20 million Americans.

The high cost of importing to the United States of America, as well as the potential for the complete harvest to be exterminated by the disease and the ubiquity of latex allergies, make domestic alternatives non-allergenic to natural rubber particularly attractive.

As an alternative to synthetic rubber sources, attention is being directed to the production of hydrocarbons in plants such as the guayule (Parthenium argentatum). Guayule is a native desert plant in the southwestern United States of America and northern Mexico and produces polymeric isoprene, essentially identical to that produced by Hevea rubber trees in Southeast Asia. Guayule plants store latex in tiny inclusions in the bark, making it desirable to collect the outer fibrous layers of the plant. The guayule normally provides half a ton to a ton of rubber per acre of cultivation and is ready to be collected and processed after only two years.

Therefore, there is a need for an economical, efficient and non-polluting method of the environment and high performance to extract and fractionate biopolymers such as rubber from plant materials such as guayule.

US 5,580,942 describes a method for preparing hypoallergenic rubber products, said method comprising a) homogenizing rubber-containing plants in an aqueous medium, wherein said aqueous medium comprises buffer, pH from about 7.0 to about 8, 0, an antioxidant and a compound that will bind phenolic compounds and resins; b) filter the homogenized product; c) separating the rubber-containing phase from the aqueous phase; and where the rubber-containing plants are non-Hevea plants.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1A is a flow chart of the initial stages of the processing system.

FIG. 1B is a flow chart of the final stages of the processing system.

DETAILED DESCRIPTION OF THE DIVERSE REALIZATIONS

The present invention uses a method of claim 4 and an apparatus of claim 1.

In various embodiments, the method can be carried out on a variety of scales, including the laboratory scale or other small scale (less than 22.7 kg (50 pounds) of plants processed per hour), pilot plant scale (typically , 22.7-227 kg (50-500 pounds) of plants processed per hour) and commercial scale (typically, more than 454 kg (more than 1,000 pounds) of plant processing capacity per hour). In one embodiment of the invention, the commercial scale variation of the process has a processing capacity of 6804 kg.

(15,000 pounds) of plants per day and a liquid capacity of approximately 12,491 l (3,300 gallons) per day using a series of high capacity tanks. Therefore, the described method can be used for small areas less than 0.2023 km2 (50 acres) of plant materials annually to an industrial scale of more than 20.23 km2 (5,000 acres) annually.

Plant materials that are used include guayule (Parthenium argentatum).

The procedure described herein extracts and purifies natural rubber from guayule plants, and the extracted rubber latex can then be processed for a variety of commercial uses, for example in the case of natural rubber, products that include articles based on latex such as gloves and latex-based medical devices.

As shown in Fig. 1A, in a typical collection process 10, plants are grown, collected and packed using conventional farm practices. With the guayule (Parthenium argentatum), the plants are harvested every two years, or at the moment when the molecular weights of the rubber are at sufficient levels to produce a sufficient amount of rubber, that is, providing an amount that makes it profitable and useful the harvest, as well as the desired levels of rubber quality. The production of rubber in plants such as guayule depends largely on environmental factors such as temperature and irrigation levels. As a result, these seasonal conditions vary from year to year and directly influence the timing and frequency of the collection process 10.

The maturity of the plants and their disposition for harvesting is determined by an assay to quantify the concentration of the latex before extraction according to the method described herein. In the guayule, the rubber particles are suspended in the cytoplasm, and the availability of water during growth directly affects the amount of the final product in the latex extraction. In cases where plants are dehydrated, the particles can be coagulated in situ, irreversibly solidifying the rubber in the plant, even after rehydration. Consequently, consistently irrigated plants contain higher levels of latex based on the cytoplasm and will generally provide a better final product. For example, if the plant contains a latex rubber concentration of 12% by weight (% in p), a high quality latex is extracted. A plant must contain at least 1% in p of latex, in order to be used in the present invention.

The collection process 10 is generally programmed based on the desired height of the plant and the weight on the basis of a scale, as well as on the moisture content based on the drying analysis. Using the guayule, the collection process 10 will not typically occur until the plants are at least one year old and have reached optimal latex concentrations for commercial scale operations. After two years, the plants typically have a height of 30-60 cm (1-2 feet) and weigh approximately 2.72 kg (6 pounds) on a wet weight basis without the root. With the root systems intact, the guayule weighs approximately 3.18 kg (7 pounds). There is no upper limit for the collection process 10 and subsequent extraction. Fully mature guayule plants (which can reach a height of 1.83 m (6 feet) and weigh more than 22.7 kg (50 pounds)) can also be processed according to the method described herein.

Using guayule, in one embodiment of the collection process 10 the plant is collected by cutting in the form of a hedge or uncoupling (by cutting the trunk of the plant above the root base) the plant, so that only the portions above the plant are collected floor of the plant and subsequently processed. In another embodiment of the collection process 10, the entire plant is unearthed and the shoots and roots are subsequently processed. In yet another embodiment of the collection process 10, the plants are partially processed in the field to form smaller pieces to allow improved packing densities when the plant is packed or encased in wheelbarrows, hoppers, containers or trucks for transportation to the plant. processing Depending on the weather conditions, guayule plants can be harvested several times. For example, a crop can be irrigated for two years before the first harvest in winter, then uncouple in spring and re-collect the following spring. When the guayule plants are cleared during the collection process 10, the plants will grow back for another collection in the future.

In various embodiments of the collection process 10, the leaves are separated from the plants in the field or separated in a processing facility. The plants can be defrosted using a mechanized cut, cut with scissors by hand, cut as a hedge or with non-dehydrating chemical defoliant. For example, defoliation can be performed using a conveyor belt system based on gravity, washing steps and / or air or water pressure to separate the sheets. An alternative embodiment of the collection process does not include defoliation of plants.

After the collection process 10, the plants are sent to a chopper 2, able to chop the pieces of the plant to a relatively uniform size or shape. The chopper 12 chopped the plants into uniform pieces to allow a separator system 14 to separate a main part of the leaves, flowers and small stems and then prepare the larger stems for debarking and wet grinding operations for the extraction of rubber from latex. The size of the chopped pieces of the plant depends on the desired scale, technique, use and the preferred final product. For example, the sizes of the pieces can range from less than 1.27 cm (1/2 inch) to greater than approximately 20.32 cm (8 inches), with an average size of 7.62-15.24 cm ( 3-6 inches) for maximized rubber extraction. If the plant is chopped too finely, latex losses will be greater due to the oxidation and dehydration of a larger specific surface of the exposed chopped plant.

The chopper 12 may include any type of chop, including mixers, mills, anvil choppers or other types of choppers. The capacity of the chopper 12 optionally reflects the desired manufacturing scale. For example, at a laboratory scale, 0.11 kg (1/4 pound) of plants could be processed per hour, while at the pilot plant scale 226.8-453.6 kg (500- 1,000 pounds) per hour. On a commercial scale, chopper 12 would be able to process 453.6 kg (1,000 pounds) or more of plants per hour.

After the chopper stage 12, in one embodiment, the chopped plants are separated by the separator system 14 in order to separate leaves, flower parts and small stems from the processing. Some or all of the sheets may be included in the processing; however, leaves, flower parts and small stems can produce undesirable results such as decreased latex stability or discoloration. Therefore, the separator system 14 is an optional stage.

An example of the separator system 14 is an air density separator which is additionally constituted by a separator chamber 16 and a blower 18 as shown in Fig. 1A. The separation stage separates most of the leaves, flower parts and small stems of a mature plant collected, which typically range from a concentration of 30-35% by weight ("% in p") in water, and do not contain rubber latex The% in p of leaves, flowers and small stems depends on the collection conditions, the annual growth of the plant, the type of plant and other factors and, therefore, this interval will only be an acceptable interval for separating leaves, parts of flowers and small stems. The range of% in p can be adjusted depending on these other conditions, or the desired product.

As shown in FIG. 1A, in one embodiment of the invention, the separator system 14 is an air density separator capable of separating the small leaves and stems from the rest of the plant within the separator chamber 16 through the forced air from the blower 18 that lifts the leaves, the parts of flowers, lighter small stems and the dirt of the heaviest bark and wood pulp of the chopped plant. The leaves, flower parts and small stems are transported by air and are collected for reuse in the biomass to the biomass collection and reuse zone 52.

In this embodiment, the blower 18 is located downstream of the separator chamber 16, so that the separator system 14 operates at a negative pressure and the air penetrates through baffles at the bottom of the separator chamber 16 under vacuum pressure. . In this embodiment, the blower 18 is also capable of forcing sufficient air capacity to lift leaves, flower parts, small stems and dirt and, in one embodiment, can be adjusted for air flow depending on the particle size wanted. For example, within the separator chamber 16, the lighter pieces (leaves, flower parts and small stems) can be separated by fluidization, internal baffles and / or flow, in which the leaves, flower parts and small stems are separated of the air and are discharged at the bottom of the separator chamber 16 through a rotary air bag feeder.

An embodiment of an air density separator system 14 for large-scale processing is a high-performance manufacturer manufactured by Carver Inc.-Lummus Corp. (Savannah, GA), which discharges larger chopped woody pieces and the bark of the bottom of the separator system 14 as feed material for further processing. For example, in one embodiment, blower 18 is adjusted to a point of lifting by bulk pressure around the weight of the whole plant and the bark paste (pressure 192-208 kg / m3 (2-3 pounds / ft3) and the weight of the leaves, flower parts and small stems (bulk pressure of 64.1-158.2 kg / m3 (48 pounds / ft3).) The separation takes place based on the difference in densities

A greater difference between the two densities makes separation easier. Optionally, additional stages of the separation system 14 can be used in cases where the difference is smaller, for example through modifications of the blower 18 adjusted with the corresponding air flow geometry and the cross-sectional velocity, based on the weights of the materials, or the scale of the separating chamber 16 to allow the material to be separated by air fluidization.

In another embodiment, the separator system 14 comprises separation by mechanical or human separation. For example, the separator system 14 may comprise hand cutting or hedge cutting of leaves and small stems in the field.

Leaves, flower parts and stems separated from the rest of the guayule plant using the separator system 14 can be sent to a biomass collection and reuse zone 52 (as shown in FIG. 1A). For example, the collected leaves and stems can be processed by a bio-refinery to form a variety of ligins or resins, and can be used in a variety of products such as bioadhesives, coatings, biopesticides, antifungal agents and antitermitic agents. The leaves, flower parts and stems can also be processed to form cellulose or hemicellulose and can be used for a variety of biofuels such as ethanol, and other bioproducts such as insulation. Any leaves, parts of flowers and stems can also be scattered again in agricultural fields in the form of mulch, or they can be combined with other by-products of the process.

Any larger pieces for further processing (eg bark, chopped plant and paste) are discharged from separator system 14 and transported to the next processing stage. Transportation methods include conventional transportation equipment that includes, but is not limited to augers, belt conveyors, hands, bucket elevators or other similar solids handling.

Latex rubber is located in the bark of chopped guayule twigs and root components. In order to increase the separation efficiency and reduce the amount of solid material processed in the latex extraction, as shown in FIG. 1A, the method may optionally include a bark separator system (or bark) 20 that follows the separator system 14. Bark separation increases the efficiency of the overall process. For example, if the bark separator system 20 is used, a higher percentage of latex is removed in the initial concentration and separation stages, reducing the need for extensive processing in later phases of the invention.

In one embodiment, the bark separation system 20 may comprise a high pressure wash or an air jet to separate the bark from the plant. The bark separator system 20 may also comprise a mechanical method for detaching the bark from the plant. The bark separator system 20 can also comprise a manual bark separation using the detachment of the bark from the plant by hand. In this embodiment, the bark is then transported to the processing facility by the conveyor, and any excess plant material is transported for refining or subsequent disposal. In further embodiments of the bark separation system 20, root systems or rootballs of the plants, or the whole plants, can be used. In one embodiment, the cortex separator system 20 can also be performed simultaneously with the stage of the separator system 14. In other embodiments, the cortex separator system 20 can be omitted.

As with leaves and stems, wood pulp that does not contain rubber, derived from the bark separator system 20, can be collected and sent to the biomass collection and reuse zone 52 for use in secondary manufacturing processes. For example, the harvested wood pulp can be processed by a bio-refinery to form a variety of ligins or resins, and can be used in a variety of products such as bioadhesives, coatings, biopesticides, antifungal agents and antitermitic agents. Wood pulp can also be processed to form cellulose or hemicellulose and used for a variety of biofuels such as ethanol, and other bioproducts such as insulation. Wood pulp can also be spread again over agricultural fields in the form of mulch or spread and planted in the form of a modification of the texture of the organic soil.

After the bark separator system 20 or the separator system 14, the plants are further processed in a chemical dissolution system 24. The chemical dissolution system 24 comprises the addition of a water-based solution to emulsify the plant material to form a plant. suspension during a stage of the grinding system 22, followed by a first press stage 26 and a washing stage 28. As shown in FIG. 1A, after the washing step 28, the chemical dissolution system 24 may further comprise passing the emulsified plant material through a second press stage 30, or further additional press stages (not shown). The chemical dissolution system 24, as described, will result in a solid product containing a biomass byproduct called "bagasse" and a suspension of the liquid homogenate containing water-based solution and diluted latex from ground plant material. In addition to water, chemical dissolution system 24 contains a buffer such as ammonium hydroxide (NH4OH), potassium hydroxide (KOH), sodium hydroxide (NaOH) or sodium bicarbonate (NaHCO3). Other buffers can also be used, for example, Tris and Trizma.

The chemical dissolution system 24 also contains, optionally, antimicrobial agents, defoaming or antifoaming agents, bleaching agents and / or stabilizers, depending on the quality of the desired product, the requirements of solubility, color or purity or sterility. In addition, antioxidants, such as sodium sulphite (Na2SO3), butylated hydroxytoluene (BHT), butylated hydroxyanisole (BHA), ascorbate, propyl gallate, alkylated diphenylamine, polybutylated bisphenol A, alkylated phenylenediamine, styrenized phenol or bisphenol can be used. sterically hindered. These antimicrobial agents, defoaming agents, bleaching agents, stabilizers and / or antioxidants can be added at various stages in the method described herein, also depending on the quality of the desired product, the requirements of stability, color, purity.

or sterility

The chemical dissolution system 24 is maintained at a sufficiently basic pH (eg greater than about pH 7.1), but not so basic as to become caustic (eg less than about pH 12.5) . Any chemical dissolution system 24 with a pH of approximately 10.0-12.0 can be used for optimized stability and an increased antimicrobial effect. Example 1 illustrates a type of chemical dissolution system 24.

The grinding system 22 comprises grinding plant material into relatively uniform pieces in a chemical dissolution system 24, as described above. In one embodiment, the milling system 22 crushes chopped homogeneous plant pieces to form an emulsified suspension with a controlled amount of chemical solution at different locations in the mill to extract the latex, which is contained in the parenchyma cells of the bark of the plants. In this embodiment, the milling system 22 forcefully divides whole or partial plant materials into smaller pieces, breaks the plant cells and allows the latex rubber to transfer to the aqueous liquid for recovery and purification. The grinding system 22 includes a wet mill and a hammer crusher as shown in Example 1.

As shown in FIG. 1A, the stage of the grinding system 22 is then followed by the first pressing stage 26 and the washing stage 28 and the second pressing stage 30, an example of which is described in Example 2. For example, the technology used in the grinding system stage 22, the first pressing stage 26, the washing stage 28 and the second pressing stage 30 may include commercially available machines such as those manufactured by Brown International (Covina, CA), Amatech Polycel, Inc. (Columbus, OH), Komline-Sanderson Filters (Ogdensburg, NJ), Andritz Bird (Austria) and USFilter / Stranco (Bradley, IL). Additionally, the technology used in the grinding system stage 22, the first pressing stage 26, the washing stage 28 and the second pressing stage 30 can be further monitored using a complete material balance to determine the amount, percentage and / or latex quality that penetrates and leaves each stage.

As shown in FIG. 1A, the next component of the chemical dissolution system 24 is the first pressing stage 26. The first pressing stage 26 separates a main part of the latex rubber from the bagasse. After the grinding system 22, the resulting latex rubber is suspended in an aqueous solution in the form of an emulsion and separated from the emulsion suspension of the biomass by squeezing the liquids from the suspension in the first press 26. The first press 26 It comprises a spindle press to squeeze plant liquids or chemical solids.

The first press 26 separates the liquid and solid phases pressed the liquid suspension through a sieve. The liquid phase, or liquid suspension of latex homogenate, passes through the sieve, while the solid phase, called the bagasse, does not pass through the sieve. The first press 26 is optimized to squeeze the maximum amount of liquid from the bagasse tightly. In one embodiment, the liquid latex homogenate suspension is collected in a recirculation tank (not shown), collection tank (not shown) or a decanter 32, and the bagasse is moved to a separate collection area, for example leaving it Drop directly into a pallet washer. Latex extraction is measured by assay, for example using a wet crusher in a closed system such as a Waring Products laboratory mixer (Torrington, CT). Depending on the amount of latex removed during the first pressing stage 26 and the desired latex yield, the washing stage 28 and the second pressing stage 30 can be omitted.

As shown in FIG. 1A, after the first pressing stage 26, in order to optimize the extraction of latex from the bagasse, a washing step 28 can optionally be used in order to separate additional latex particles trapped in the bagasse after the First pressing stage 26. In at least one embodiment, the washing stage 28 uses a water tank with a charge pump capable of pressurizing the feeds in the machinery, allowing the water to interface with any suspension of homogenized latex from resulting liquid phase that is released by washing the bagasse. For example, in this embodiment, the liquid phase latex homogenate suspension is pumped to the vane mixer using solenoids. Generally, the extraction method described herein preferably contains the lowest possible number of washing steps 28 (typically less than two washing steps 28) in order to minimize the use of water through the system.

As shown in FIG. 1A, in some embodiments in which the optional wash stage 28 is included, and the bagasse is passed through the second press stage 30 for further processing, the second press stage 30 may use a sieve or size of smaller filter compared to the first pressing stage 26, depending on the desired results. The second press stage 30 is used to extract a higher yield of latex from the bagasse. The liquid containing the latex rubber is collected separately in a collection tank or sent to the decanter 32.

During the second press stage 30, any remaining latex homogenate suspension is separated by pressing the bagasse by the second press 30, and any resulting liquid is again separated from any remaining solids. The liquid phase is pumped to a collection tank or decanter 32, while the solid phase bagasse drips to another collection zone. The second press stage 30 may optionally be followed by a washing step, and additional press stages (not shown) may be repeated. The quantification tests are carried out after each of the press stages, and again after the final press stage (eg the second press stage 30).

After the final press stage (eg the second press stage 30), the bagasse is collected and moved to a biomass collection and reuse zone 52 for use such as in secondary manufacturing processes that include extraction of resins, fuels, chipboard boards and ethanol. For example, bagasse can be processed by a bio-refinery to form a variety of ligins or resins and used in a variety of products such as bioadhesives, coatings, biopesticides, antifungal agents and antitermitic agents. Bagasse can also be processed to form cellulose or hemicellulose and used for a variety of biofuels such as ethanol, and other bioproducts such as insulation. Other products produced at this stage of secondary manufacturing may include fuel nodules, logs for chimneys, roofing tiles, building materials, equipment for sports grounds and flooring. Any bagasse, either intact or devoid of resin, can also be spread again over agricultural fields in the form of mulch or sold commercially in the form of mulch.

As shown in FIG. 1B, after the final press stage (eg the second press stage 30), and the separation of the bagasse to the biomass collection and reuse zone 52, the resulting liquid latex homogenate is then optionally transferred to a collection tank (not shown) or decanter 32.

Despite being optional, the decanter stage 32 separates the maximum amount of undesirable solids in the latex, while retaining the maximum amount of latex. The decrease in the amount of undesirable solids increases the efficiency by reducing the binding in later stages (eg the first press stage 28 and / or the second press stage 30). For example, without the decanter stage 32, solids not separated from the latex can eventually shorten the operating cycles and can cause undesirable downtime and loss of latex. Undesirable solids can also affect the storage and stability of the latex.

The transfer to the decanter 32 can be directly from the last stage of the spindle press (eg the second press stage 30), from a recirculation or storage tank, directly from the first press 26 or from a combination of these sources (eg a combination of homogenate from the first press 26 and the second press 30) that are mixed together before decanting.

In an alternative embodiment, the homogenate from the first press stage 26 is further processed, while the homogenate from the second press stage 30 is recirculated to the stage of the grinding system 22 in the form of a means of aqueous milling, after which all homogenate with resulting latex content is cycled to the decanter 32. The decanter 32 may comprise a centrifuge, tank or other separator.

The decanter 32 may include any physical or mechanical phase separation systems, used to separate the latex containing the liquid phase from waste products containing a solid phase, consisting of fine non-rubbery particulate materials that were not separated into previous stages. Examples of decanter 32 include centrifuge decanters manufactured by Westphalia (Germany), Alfa Laval (Sweden) and Sharples (United Kingdom). For example, in one embodiment, a centrifuge-based decanter process 32 may separate approximately 80-85% of undesirable solids without separating any latex, in approximately 30 seconds of centrifugation. Centrifugal decanters 32 provide the benefits of continuous operation and rapid solids separation, but these are not the only type of decanter 32 capable of carrying out this stage. In other embodiments, other types of decanter equipment 32 can be used for decanting such as other filtration systems (eg a filter or a series of filters driven by a belt system) or other processes.

During decantation, the homogenized liquid containing latex (collected from any of the steps 22-30 previously described) is passed through the decanter 32 to separate coarse vegetable solids from the emulsion liquids of the latex. Decanter 32 separates solid materials from liquid phases (eg through centrifugation). In various embodiments, optional additives such as stabilizers, antifoaming agents or defoaming agents can be added to the clarified liquid latex homogenate during or after the decanter stage 32, in order to reinforce the specific chemical or physical properties of the latex particles. during subsequent treatment using centrifugation. In alternative embodiments of the invention, no stabilizing compounds are added.

Bagasse solids from decanter 32 can be collected for use as a feedstock for secondary manufacturing processes, including resin extraction, fuel, chipboard and ethanol. Bagasse solids that are collected in the solids collection and reuse zone 52 can be combined with bagasse, bark, leaves or stems collected in previous stages, used separately as feedstock for secondary procedures, or can be Discard.

In various embodiments, the decanter 32 also has the ability to dehydrate the liquid. Dehydration involves separating water or other aqueous wastes from the latex to the wastewater recovery zone 54 in order to effectively concentrate the emulsion of the latex rubber. In such an embodiment, a concentrated latex emulsion stream exits the decanter 32 and is transferred to a storage vessel (not shown) for maintenance, or sent directly to a first separator 34.

As shown in FIG. 1B (an example which is described in Example 3), after the stage of the decanter 32, the homogenized liquid containing latex is fed to a series of separators, including the first separator 34, a first latex concentrator 36 and a second latex concentrator 38. Steps 3438 are optionally carried out to further separate fine solids from the emulsion and concentrate the latex rubber emulsion, separating water or other aqueous waste to the wastewater recovery zone.

54. Particles of finer-sized solids, which were not separated by the decanter 32, are separated by the first separator 34. The first separator stage 34 prevents the binding in the first latex concentrator 36 and the second concentrator 38 latex

The first separator 34 may consist of any physical or mechanical phase separation system used to separate a latex containing the light phase and waste products containing the heavy phase. Depending on the desired quality and production requirements, after the first separator stage 34, the latex containing the resulting light phase can be further concentrated in one or more concentrator stages. For example, the latex containing the light phase is further concentrated in a first latex concentrator 36 and in a second latex concentrator 38 such as an Alfa Laval Latex 2000 high speed centrifuge.

However, it is understood in one embodiment that a single latex concentrator is used, while in other embodiments multiple latex concentrators are used for multiple concentration steps. It is also understood that multiple stages of latex concentration can be carried out in a single latex concentrator. In another embodiment, two latex concentrators are used to carry out three or more stages of latex concentration. For example, second and third concentrations are made using the second latex concentrator 38, as illustrated in Example 4.

In the first latex concentrator 36 and / or the second latex concentrator 38, the light phase may be mixed with an additional chemical solution, as more specifically described in Example 3. In various embodiments, the latex containing the light phase it can be stored in one or more intermediate tanks (not shown in FIG. 1A or 1B), between the stage of the first separator 34, the stage of the first latex concentrator 36 and / or the stage of the second latex concentrator 38. In various embodiments, the first latex concentrator 36 and / or the second latex concentrator 38, individually or both, have a discharge characteristic to release the accumulated solids in order to avoid clogging.

The first latex concentrator 36 comprises any chemical or mechanical phase separation system used to separate water and concentrate the latex emulsion such as by high speed centrifugation. In one embodiment, the first latex concentrator 36 is a custom high speed centrifuge, specifically made for latex concentration, such as centrifuge concentrators of the high speed latex of Alfa Laval and Westphalia. During this stage, chemical solutions can be added to improve the quality of the latex. For example, in the first latex concentrator 36, the latex rubber emulsion can be diluted with a chemical solution to help separate soluble proteins and / or other impurities and to separate additional water, and then it can be concentrated by centrifugal separation. .

As shown in FIG. 1B, the wastewater and impurities from the first latex concentrator 36 are transferred to the wastewater recovery and reuse zone 54. After leaving the first latex concentrator 36, the concentrated latex rubber is then optionally transferred to the storage (not shown) and analyzed for the concentration and quality of the product. If the product is sufficiently concentrated and the soluble proteins and other impurities have been adequately separated, after the first latex concentrator 36, based on latex assays as shown in Example 7, it will be transferred to a storage system 50 of the final product for transport to buyers. In cases where additional concentration and / or purification is required, the product will be sent to the second latex concentrator 38.

As with the first latex concentrator 36, the second latex concentrator 38 also comprises any physical or mechanical phase separation system used to separate the water and concentrate the latex emulsion, such as by high speed centrifugation. In one embodiment, the second latex concentrator 38 is also a custom high speed centrifuge, specifically made for latex concentration, such as Alfa Laval and Westphalia high speed latex centrifuge concentrators. During this stage chemical solutions can be added to improve the quality of the latex. For example, in the second latex concentrator 38, the latex rubber emulsion can be diluted with a chemical solution to help separate soluble proteins and other impurities and to separate additional water, and then concentrate by centrifugal separation. As shown in FIG. 1B, the wastewater and impurities from the second latex concentrator 38 are also transferred to the wastewater recovery and reuse zone

54. The performance in the emulsion is measured using the total solids content of the latex in mg / ml, gravimetrically dried and weighed, as described in greater detail in Example 3.

After leaving the second latex concentrator 38, the concentrated latex rubber is then transferred for storage (not shown) and analyzed for product concentration and quality. If the product is sufficiently concentrated and soluble proteins and other impurities have been adequately separated, after the second high-speed latex concentrator, the product will be transferred to a storage of the final product for shipment to consumers in various packages. After the concentration of the latex, the resulting latex product is ready for a processing use in which it has a pH range of approximately pH 8.0 to pH 11.0 and a dry rubber content ("DRC"). in English) of more than 40%, based on conventional test techniques, for example as described in Example 3.

For general processing uses such as glove production, the DRC of the latex product is considered acceptable when the weight to volume ratio is equal to or greater than 40%. For example, a 100 ml aliquot of liquid latex that results in 40 g of dry rubber when dried would have a DRC of 40%. If the latex emulsion requires an additional concentration, the material will be further concentrated using centrifugation, or it will be transferred as a feed for the cream-forming stages 40-46 of the process.

The cream formation system comprises cream formation stages 40-46, as shown in FIG. 1B, of which one embodiment is further described in Example 5. The cream formation system fulfills a function similar to the concentration system described in steps 34-38. Both systems are additional concentration steps that increase the concentration of the latex without affecting the concentration of the soluble components in the aqueous phase of the latex. Both systems increase the volume of the latex, while decreasing the aqueous volume, and both systems require several dilutions that separate solutes and re-concentrated latex. However, effective separations with centrifuges become impractical after soluble components and colloidal stabilizers drop below certain levels. At a certain level, the latex is so "clean" that it coagulates under centrifugal force, making it necessary to add potent surfactants or the concentration of non-shear forces.

The cream formation process allows additional washing and re-concentration using normal gravity, if necessary, after centrifugation has become impractical. In an example of the system, the cream-forming stages 40-46 are carried out in a series of cylindrical stainless steel containers, with a conical bottom, straight, vertical walls and 6056 l (1600 gallons). In other embodiments, other types of containers may be used.

As shown in FIG. 1B, the mixing system 40 of the cream-forming solution is constituted by equipment to prepare batches of solution to be added to the cream mixing tank 42, followed by a first cream settling system 44 and a second settling system of Cream 46. Cream settling systems and additional and optional cream mixing tank stages 42 (not shown in FIG. 1B) can optionally be performed depending on the desired results. After the final settling system, the remaining latex supernatant layer is transferred to an area 48 of the latex product tank where the final product is tested to determine the pH range and dry rubber content.

The solution in the cream dissolving mixing system 40 consists of a coagulant, various stabilizers and an antioxidant. The cream solution mixing system 40 allows the emulsion of the latex rubber to phase out with the water until it reaches the desired concentration (eg a concentration of 50-60% by weight of latex rubber in water) and also separates undesirable proteins and impurities. The content of the cream solution mixing system 40 is pumped into the cream mixing tank through various methods, for example, by discontinuous transfer.

Cream mixing tank 42 is a container for additional latex concentration. In one embodiment, the cream mixing tank 42 is a stirred vessel with heating and cooling to control the temperature. In one embodiment, the temperature is maintained between 20-30 ° C. According to other embodiments, cream formation will occur at temperatures outside this range or without temperature controls.

In one embodiment, the contents of the cream dissolving mixing system 40 and the product of the stage of the second latex concentrator 38 are gathered in the cream mixing tank 42. In this embodiment, the combined content of the cream mixing tank 42 is then stirred for thorough mixing, and the temperature is adjusted to the range of 20-30 ° C.

As shown in FIG. 1B, after stirring in the cream mixing tank 42, the content is then transferred to a first cream settling system 44. In one embodiment, the first settling system of cream 44 comprises one or more isolated, non-stirred tanks. , isolated to maintain an internal temperature of the content of 20-30 ° C. In other embodiments, the first cream settling system 44 is produced at temperatures outside this range, or without temperature controls.

The duration of the first cream settling system 44 depends on the volume of the tanks and other environmental factors. The first cream settling system 44 is completed after the bottom aqueous phase (typically brown) separates from the upper latex rubber phase (typically greenish). The aqueous layer is decanted to the wastewater recovery and reuse zone 54. The upper layer containing a latex rubber phase is transferred back to the cream mixing tank 42 in which the latex rubber phase is mixed with again with an additional cream dissolving mixing system 40 consisting of a coagulant, various stabilizers and an antioxidant.

As shown in FIG. 1B, after the second stirring period in the cream mixing tank 42, the content is then transferred to the second cream settling system 46 which also comprises one or more insulated and non-stirred tanks, isolated to maintain an internal temperature of the content from 20-30 ° C. In one embodiment, the second cream settling system 46 comprises one or more insulated and non-stirred tanks, isolated to maintain an internal temperature of the content of 20-30 ° C. In other embodiments, the second cream settling system 46 is produced at temperatures outside this range, or without temperature controls.

The duration of the second cream settling system 46 also depends on the volume of the tanks and other environmental factors. Again, the second cream settling system 46 separates the latex rubber emulsion from the water and separates undesirable proteins and impurities. As before, the aqueous layer is decanted to the wastewater recovery and reuse zone 54. The upper layer containing a latex rubber phase is transferred to the tank area of the latex product 48 for testing and, finally, it is transferred to the final product storage system 50.

The physical properties and composition of the latex product can be monitored in one or more phases in the process, as described above (eg after the second press 30, after the decanter stage 32, after the first separator stage 34, after concentration, after cream formation or in other phases in the process). Example 7 shows a test method.

Generally, any latex extracted for industrial or medical uses, including that of the present description, is tested for compliance with the specifications for the standards of the American Society for the Testing of Materials ("ASTM") for D1076- 02, as shown in Table 1 below. Specifically, Table 1 shows the standard D1076-02 standard for Natural Latex Concentrated in Rubber, Preserved in Ammonia, Creamy and Centrifuged. In one embodiment, the extracted latex conforms to type D1076-02

1. In another embodiment, the latex conforms to D1076-02 type 3.

Kind

Description

Type 1

Natural latex centrifuged, preserved with ammonia only or by formaldehyde followed by ammonia

Type 2

Creamy natural latex, preserved with ammonia only or by formaldehyde followed by ammonia

Type 3

Natural centrifuged latex, preserved with low ammonia content with other necessary preservatives

Table 1

5 In other embodiments, the extracted latex conforms to the specifications included in the ASTM standard values for natural rubber latex, including total solids, dry rubber content, alkalinity, viscosity, sediment content, clot content, index of KOH, pH, stability, copper and manganese levels, density, volatile fatty acids and the like, as shown in Table 2 below. In others

10 embodiments, the specific properties and characteristics of the extracted latex differ from those listed in the ASTM D1076-02 specifications. For example, this may be due to differences in the inherent properties between the source of latex derived from Hevea, towards which conventional values are directed, to values of a latex source not derived from Hevea.

fifteen

Properties

KOH buffered latex product KOH buffered latex product Ammonialed latex product Ammonialed latex product

Final Processing Stage

Centrifuged Centrifuged and with cream Centrifuged Centrifuged and with cream

Total solids content (%)

48.0 54.0 48.0 54.0

Dry rubber content (%)

47.0 53.0 47.0 53.0

Total alkalinity, KOH as% latex

0.10 0.40 0.10 0.40

Viscosity at 43% TSC, cps

20.0 150.0 20.0 150.0

Sediments,% by weight

- 0.07 - 0.07

Clot,% by weight

- 0.02 - 0.02

pH

11.0 13.0 11.0 13.0

Mechanical stability at 43% TSC, seconds

100.0 600.0 100.0 600.0

Copper (ppm)

- 6.0 - 6.0

Manganese (ppm)

- 6.0 - 6.0

Density (mg / m3)

0.940 0.960 0.940 0.960

Color

whitish, beige whitish, beige whitish, beige whitish, beige

Odor

without smell without smell mild smell of ammonia mild smell of ammonia

Table 2

The purity of the final latex product is tested by determining the concentration of the protein in the aqueous phase of the latex, through conventional techniques such as the analysis of latex proteins according to ASTM

20 D5712 and the analysis of Hevea antigenic proteins according to ASTM 6499. The overall purity or composition requirements depend on the use of the final latex product; however, generally, a reference standard for the final product includes general conformation to ASTM D1076-02 standards or a percentage of dry rubber content above a latex rubber concentration of 40% by weight in water.

ASTM specification quality latex can be stored in the final product storage system 50 in stirred tanks at 4 ° C for an indefinite period of time. Stabilizers or other agents may be added depending on the performance requirements of the downstream product. The latex can be packaged in individual transport containers, or transported in bulk in refrigerated trucks, tankers, barges, wagons and the like. Typical applications of the method described herein include surgical or reconnaissance gloves, medical adhesive, latex products for wound care, catheters or other medical equipment or devices in which a clinically proven solution to the serious health risks imposed by Tropical rubber latex.

Example 1: Sintering and milling of the ammonia antioxidant chemical solution

A water-based ammonia antioxidant solution (“AAO”) containing 695 mL / L of ammonium hydroxide (NH4OH) and the 1 g / L sodium sulfite antimicrobial bleaching agent (Na2SO3) is mixed with water by injection. AAO is stored at a pH of 10.5 in 189 l (50 gallon) tanks, or is processed alternately through the system without storage, at a pH of 10.0. The AAO is pumped to the grinding system 22 through the use of solenoids and is assembled with materials from the guayule plant in a wet mill. The plant materials are emulsified to form a suspension. The milling system 22 comprises a wet mill and, more specifically, an MP-30 crusher from Schutte-Buffalo Pulverizer Co. (Buffalo, NY), which accepts plant material, transported to an MP-30 hopper and cuts to the plant in relatively uniform pieces of 7.62-15.24 cm (3-6 inches). The grinding system 22 further comprises a belt conveyor that transfers the crushed guayule pieces to a Shutte-Buffalo 1320 hammer crusher for hammer crushing.

Example 2: Grinding system and pressing stages

Following the steps of the milling system 22, described in Example 1, the guayule plant materials are pressed in a first press stage 26, which comprises a helical auger and a Brown International spindle press, which presses the liquid suspension through a sieve to separate the liquid phase, the AAO / latex homogenate diluted from the solid phase. The solid phase bagasse does not pass through the sieve. The dilute AAO / diluted latex liquid homogenate suspension is collected in a recirculation tank and the bagasse drips directly to a pallet washer from Compak Systems, CS Processing Engineering Ltd. (Lincoln, England).

Any remaining latex particles are separated by washing the bagasse in the Compak Systems pallet washer using a pressurized stream of water from a water tank. More specifically, the water tank used in the washing stage 28 has a charge pump attached to a high pressure solenoid source, which interfaces the water with the homogenate material and pumps the AAO / latex homogenate into the washing machine of Compak Systems pallets.

After the washing step 28, the guayule plant materials are then pressed in a second press stage 30, which comprises passing the diluted AAO / latex homogenate suspension to another spindle press in which the liquid separates again of any remaining solids. The resulting diluted AAO / latex homogenate is pumped into a recirculation tank, while the bagasse drips into a helical auger from Com-Pak International.

Finally, the AAO / diluted liquid latex homogenate in the recirculation tank is pumped to a decanter 32 of Alfa Laval (Sweden), where the latex homogenates from the first press 26 and second press 30 stages are mixed together before being treated further. The bagasse from the first press stage 26 and the second press stage 30 is also combined in the biomass collection and reuse zone 52, and subsequently processed for other secondary uses. Polymeric flocculating agents, stabilizers and antifoaming agents are added to the homogenate liquid of AAO / latex diluted in the decanter 32 for increased stability and decreased foaming.

Example 3: Separation and concentration

After the pressing and settling steps, as described in Example 2, the latex homogenate is measured to determine the percentage of latex present (desirably, approximately 0.01% to 1% after settling) and transfer from the decanter 32 to the first separator 34, a high speed centrifuge Alfa Laval PX-510, and centrifuge for approximately 15 seconds or less.

The first separator 34 separates the latex homogenate into a latex containing a light phase and waste products containing a heavy phase. The heavy phase is removed from the wastewater recovery zone 54 in which the waste products are recycled for use as a milling medium or for further cleaning using conventional water purification treatments. After the first separator 34, the latex homogenate is measured to determine the percentage of latex present. Preferably, this is about 1% after the first separator stage 34.

After being separated in the first separator 34, the latex containing a light phase is pumped to an intermediate tank (not shown in FIG. 1B) and mixed with AAO through an AAO tank (not shown in the FIG. 1B) that flows directly to the intermediate tank. The light phase is then pumped to the first latex concentrator 36, a high speed Alfa Lavel Latex 2000, optimized for guayule latex, in order to further concentrate the latex. Excess amounts of the latex containing a light phase, which passed through the system, are restarted by pumping the light phase to another intermediate tank where it is mixed with additional AAO, through an AAO tank that flows directly to an intermediate tank (not shown in FIG. 1B). The latex homogenate is then tested to determine the percentage of latex present, desirably, about 10% or more at this point.

The homogenate is then run through the second latex concentrator 38, a high speed Alfa Laval Latex 2000, optimized for the guayule latex. After this stage of the second latex concentrator 38, the pH is tested and determined. Typical results for the stage of the second latex concentrator 38 are a latex product with a final pH of approximately 10.5. The dry rubber content is then determined gravimetrically, where an aliquot of the liquid latex, of known volume, is dried to substantially separate all moisture content and is weighed, and a determination is made as to whether the material requires a further processing with the cream formation system, as described below. After the stage of the second latex concentrator 38, the percentage of latex present is desirably about 40 to 50% or more.

Example 4: Concentration in three steps

In some embodiments of the present description, more than two concentrations, also called "steps", are made through a latex concentrator. In one embodiment, a third concentration is performed. In one example, this third concentration, which is also referred to here as the "third step" is performed with the second latex concentrator 38, a high speed Alfa Laval Latex 2000 optimized for guayule latex. In this example, the latex is collected and an additional 16: 1 dilution of AAO and surfactant is added to the light phase from the second concentration (or second step) in a tank, and a dilution

32: 1 that was previously diluted at a ratio of 5: 1.

In this example, the latex subnatant from the third step was a much more translucent color than the second step. The light phase of the third step resulted in a total solids content of approximately 55%. According to this example, the maintenance of a 16: 1 dilution of latex is preferably carried out in a third step.

Example 5: Cream Formation

After the steps described in Example 3, the test may indicate that the product requires an additional concentration. Latex containing light phase is pumped into a cream mixing tank 42 of 397 l (105 gallons) and combined with a cream solution mixture containing 0.1% sodium alginate from the cream dissolving mixing system 40. After this mixing stage, the content is transferred to the first cream settling system 44, and it is allowed to settle in an isolated and non-stirred tank, isolated to maintain an internal temperature of the content of 20-30 ° C. After sedimentation, the subnatant aqueous residual layer is drained to the wastewater recovery and reuse zone 54. The remaining latex supernatant layer is transferred back to the cream mixing tank 42, in which the mixing tank of cream 42 is filled with 0.1% sodium alginate solution and mixed. After this mixing stage, the content is transferred to the second cream settling system 46 and allowed to settle in a non-stirred tank, isolated to maintain an internal content temperature of 20-30 ° C. After sedimentation, the subnatant aqueous residual layer is drained back to the wastewater recovery and reuse zone 54. These steps are repeated, as necessary, to wash the soluble latex proteins. In cases where the cream mixing tank 42 is filled six times to further concentrate the latex and separate the subnatants, a latex product with a final pH of approximately 10.5 was found.

In various embodiments, the procedures described herein are monitored by a control system (not shown in FIGS. 1A or 1B), an example of which is described in Example 6. In various embodiments, this control system will regulate and / or monitor the temperature, process conditions, volume, entry and exit of water or chemicals, product exit and / or waste collection through a series of pumps, computers and flow meters, as required by the specific system.

Example 6: Control System

An example of the control system for the procedure described herein is through a Motor Control Center ("MCC" - Motor Control Center), linked to a Programmed Logic Center ("PLC"). The PLC controls the start and stop of the machinery, although the machines are also capable of being manually controlled. Multiple pH meters of Yokogawa (Japan) are linked to the PLC. Locations for pH meters include dissolution tanks, collection tanks and in the recirculation tank for the pallet washer.

Ammonium hydroxide is pumped directly to the pH meter locations using a metering pump. A flow of ammonium hydroxide is controlled with the use of solenoids linked to the PLC. The pipes connecting the ammonium hydroxide tanks are also connected to the final intermediate tank before the cream formation, in order to control the final pH, and this pipe is controlled either manually or automatically by the PLC.

Within the system six flow meters are present. These include two Omega turbine flow meters (Stamford, CT) FTB792 to monitor and adjust the flow. The Omega FTB792 turbine flowmeters are placed at the solenoid-ammonium hydroxide / water R / O connection, and the sodium sulfite / water / R / O pipe connection. At the point of connection, ammonium hydroxide and sodium sulphite are mixed with water for injection.

An additional Omega FPR 132 turbine flowmeter regulates the water outlet for the mixture and provides accurate information on the amount of liquid present in the system throughout the process. In addition, the system also contains three additional flowmeters, more specifically PROline Promag 50/53 magnetic flowmeters from Endress Hauser (Switzerland) to monitor the homogenate.

The system also contains multiple pumps, which include variable speed input pumps, linked to the PLC, and all single speed output pumps. Additionally, the water system throughout the process has a high water flow that utilizes an R / O high pressure system from Advanced Water Systems (Santa Cruz, CA), with a flow of approximately 45.42-52.99 l / min (12-14 gallons / minute). Water is softened as necessary with sulfuric acid in order to maintain an optimal water flow.

Example 7: Test Patterns

After the steps described in Examples 1-4, the analysis of the latex proteins according to ASTM is performed in accordance with the ASTM D5712 protocol and compared with ASTM D1076-02 standards. The latex compound derived from guayule is measured to determine the final composition of each ASTM parameter. As shown in FIG. 1B, the purity of the final latex product is tested by determining the concentration of the protein in the aqueous phase of the latex in various batches, indicating a total rubber content of approximately 4854%, a dry rubber content of approximately 47-53% and a total alkalinity (KOH as% of latex) of about 0.10 to 0.40%. Guayule-derived latex product meets or exceeds ASTM standards, and is ready for subsequent secondary packaging, storage or manufacturing to form derived products. It is further envisaged that the process described herein can be modified to include additional steps such as flocculation processes, a variety of pumping systems such as positive displacement pumps, a variety of crushers, centrifuges, vibratory screening technology, presses

5 spindle, vacuum pumps, diesel separation systems, modifications of chemical cream formation formulations, and the like. Similarly, a certain number of stages described in the process can be omitted or reordered based on the desired product and the individual characteristics of the plant materials.

The foregoing description of a preferred embodiment and the best mode of the invention known by the applicant at the time of submitting the application have been submitted and is intended for the purposes of illustration and description.

Claims (12)

1. An apparatus for extracting a rubber latex from a non-Hevea plant material, wherein the plant material is guayule, comprising: a hammer crusher (22) wherein the hammer crusher is capable of mixing crushed plant material with a buffer and water to form a ground product consisting of a bagasse and a liquid homogenate; a spindle press filtration system (26), fluidly coupled with the hammer crusher, wherein the spindle press filtration system is capable of separating the ground product in the bagasse and the liquid homogenate; a homogenate storage tank, fluidly coupled to the spindle press filtration system, wherein the homogenate storage tank is capable of storing a liquid homogenate consisting of ground plant material, the buffer and water; a phase separation system (34) fluidly coupled to the homogenate storage tank, wherein the phase separation system is capable of separating the liquid homogenized product in a light phase and a heavy phase; Y a biopolymer storage tank, fluidly coupled with the phase separation system, where the biopolymer storage tank is capable of storing rubber latex. 2. The apparatus of claim 1, further comprising a biopolymer concentrator (36, 38) fluidly coupled to the phase separation system, wherein the biopolymer concentrator is capable of producing rubber latex from the light phase 3. The apparatus of claim 1 or 2, further comprising a cream-forming system (40, 46) fluidly coupled to the biopolymer concentrator, wherein the cream-forming system is capable of concentrating the latex of rubber and separate subnatants from the light phase. 4.- A method to extract rubber latex from a non-Hevea plant material, in which the plant material It is guayule, using the apparatus of claim 1, comprising: crush a plant material; grind the plant matter in a chemical solution that includes water and a buffer, whereby grinding results in a ground product consisting of a solid bagasse and a liquid homogenate, wherein the liquid homogenate includes ground plant material, a buffer and water; filter the solid bagasse from the liquid homogenate; separating the liquid homogenate in a light phase and a heavy phase; purify the light phase, where soluble proteins are separated; Y concentrate the light phase, where the concentration of the light phase produces rubber latex. 5. The method of claim 4, further comprising washing the bagasse, whereby additional rubber latex particles are separated from the bagasse. 6. The method of claim 4, wherein the chemical solution further includes one or more agents selected from the group consisting of: a stabilizer, a polymeric flocculating agent, an antimicrobial agent, a defoaming agent, an agent of bleaching and an antioxidant. 7. The method of claim 4, further comprising using bagasse in a secondary manufacturing process, wherein the secondary manufacturing process is selected from a group consisting of: resin extraction, ligin extraction, Cellulose treatment and hemicellulose treatment. 8. The method of claim 7, wherein the secondary manufacturing process provides a product selected from the group consisting of: resin, ligin, adhesive, pesticide, an antifungal agent, ethanol, a chipboard, insulation, mulch , a modification of the texture of the organic soil, fuel nodules, logs for chimneys, roofing tiles, building materials, equipment for sports fields and flooring. 9. The method of claim 4, further comprising decanting the liquid homogenate that includes centrifugation, wherein the additional solid bagasse is separated. 10. The method of claim 4, further comprising separating water from the liquid homogenate. The method of claim 4, wherein the purification of the light phase includes mixing it with ammonia antioxidant. 12. The method of claim 4, further comprising transforming the light phase into cream using a A cream solution consisting of a coagulant, an antioxidant and a stabilizer, in which the light phase cream conversion includes concentrating the rubber latex and separating subnatants from the light phase. 13. The method of claim 4, wherein the plant material includes more than one percent of the rubber latex. fifteen